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CN108461781A - The method and fuel cell system of starting fluid battery apparatus - Google Patents

The method and fuel cell system of starting fluid battery apparatus Download PDF

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Publication number
CN108461781A
CN108461781A CN201810151082.8A CN201810151082A CN108461781A CN 108461781 A CN108461781 A CN 108461781A CN 201810151082 A CN201810151082 A CN 201810151082A CN 108461781 A CN108461781 A CN 108461781A
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CN
China
Prior art keywords
fuel
gas
heat exchanger
fuel cell
burner
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Granted
Application number
CN201810151082.8A
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Chinese (zh)
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CN108461781B (en
Inventor
J·舒尔勒
G·科尔布
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Diehl Aerospace GmbH
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Diehl Aerospace GmbH
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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04223—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells
    • H01M8/04268—Heating of fuel cells during the start-up of the fuel cells
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
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    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
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    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
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    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
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    • H01M8/04022—Heating by combustion
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    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
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    • H01M8/04223—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells
    • H01M8/04225—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells during start-up
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    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/043—Processes for controlling fuel cells or fuel cell systems applied during specific periods
    • H01M8/04302—Processes for controlling fuel cells or fuel cell systems applied during specific periods applied during start-up
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    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
    • H01M8/0432—Temperature; Ambient temperature
    • H01M8/04373—Temperature; Ambient temperature of auxiliary devices, e.g. reformers, compressors, burners
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    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
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    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04701—Temperature
    • H01M8/04738—Temperature of auxiliary devices, e.g. reformer, compressor, burner
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    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
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    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
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    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
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    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
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Abstract

The present invention relates to the method for starting fluid battery apparatus, fuel cell system includes fuel processor and fuel cell, and fuel processor includes following element：First evaporator, reformer, water-gas shift reaction device, PrOx reactors, first heat exchanger, afterburner and startup burner, this method include：Heating equipment in electrical heating fuel processor, to heat first gas；The first gas of heating is set to cycle through at least first heat exchanger and afterburner and the element of fuel processor is heated to fixed operation temperature；The fuel of catalysis burning atomization or evaporation in starting burner, then the afterburning hydrogen in afterburner, is used to further heat first gas；It introduces the fuel into the pre-add thermal element of fuel processor and stops starting the catalysis burning in burner；Start reaction in the element of fuel processor, until the gas come out from PrOx reactors has given CO contents；Connect fuel cell.The invention further relates to fuel cell systems.

Description

The method and fuel cell system of starting fluid battery apparatus
Technical field
The present invention relates to a kind of method of starting fluid battery apparatus and a kind of fuel cell systems.
Background technology
It there is known a kind of method of starting fluid battery apparatus and a kind of fuel from such as 203 20 913 U1 of DE Battery apparatus.Known fuel cell system includes fuel reservoir, heating unit and fuel-cell device.Heating unit is to pass through Generate hot water and/or hot-air and be performed separately with fuel-cell device and can dedicated for starting fluid cell apparatus plus Hot cell.Fuel cell system can utilize the main fuel being made of butane or propane to operate, and butane and propane generally also can be used In gas burner.In addition, fuel cell system may include carrying out pre-warmed latent heat to fuel cell after restarting Storage facility.In this case, reformer is heated first, is then added fuel cell by the gas heated in reformer Heat.
Alternatively, DE 203 20 913 further discloses a kind of operable heating unit of utilization electricity.In addition, the disclosure Document contemplates other heat sources for being heated to reformer and fuel cell, especially electric heat source.The system proposed It is bulky and needs big quantity space.In addition, it is not suitable for the fuel cell using propylene glycol operation.
1 703 578 A1 of EP disclose a kind of reformer/fuel cell system and one kind with external burner Start the method for the reformer/fuel cell system.The startup of the reformer/fuel cell system needs to be arranged in exterior Burner for generating heat discharge gas.The discharge gas generated in this way is conducted through one of reformer/fuel cell system Point, in order to which the element of reformer/fuel cell system is heated to given temperature.It is arranged dedicated for starting the combustion of the system Burner means that the system needs additional burner, thus has increased volume.In addition, after startup stage terminates, It must be prevented from process gas and flow back into the valve for starting in burner, thus needing additional.In addition, the frequent landform in the burner At soot particle, the soot particle can be deposited in the reformer system in downstream.Soot particle, which covers catalyst coatings, reduces catalyst coatings Efficiency and the service life, and reduce in heat exchanger it is possible heat transmit.This dramatically increases the maintenance needs of the system.
Invention content
Problem to be solved by this invention is to eliminate defect in the prior art.More particularly, one kind is described in detail has The element of the method for the starting fluid battery apparatus of effect, the fuel cell system can also be in the maintenance of the fuel cell system It is used in operation.
Problem to be solved by this invention passes through the method and fuel according to the present invention for starting fluid battery apparatus The feature of battery apparatus solves.
According to the present invention, the fuel cell system that a kind of startup includes fuel processor and fuel cell is described in detail Method, wherein fuel processor includes following element：Evaporator, the reformer for being arranged in evaporator downstream, water-gas shift are anti- It answers device, PrOx reactors, first heat exchanger and starts burner, wherein this method comprises the following steps：
A) heating equipment in fuel processor is electrically heated, first gas is heated,
It b) will be at fuel by making the first gas heated cycle through at least afterburner and first heat exchanger The element of reason device is heated to fixed operation temperature,
C) fuel that catalysis burning is atomized or evaporates in starting burner, then the afterburning hydrogen in afterburner, is used In further being heated to first gas via at least one heat exchanger,
D) it introduces the fuel into the pre-add thermal element of fuel processor, and stops starting the catalysis burning in burner,
E) start at least one reaction in the element of fuel processor, until the gas come out from PrOx reactors has Given CO contents, and
F) fuel cell is connected.
" fuel processor " is construed as meaning a kind of concatenated reactor apparatus, wherein fuel passes through wherein One or more reaction is converted, to generate the gas containing hydrogen that be directed into fuel cell.It is anti-at these Ying Zhong, it is accordingly required in particular to, CO contents are reduced to given content.Particularly, suitable fuel is propylene glycol.First gas packet It is oxygenous.Fuel processor includes the evaporator that fuel is evaporated wherein.Preferably, by propylene glycol/water in evaporator Mixture evaporates.Here " evaporation " also means to generate superheated steam.
One fuel processor element is reformer.In reformer, the fuel of evaporation, second gas and addition first Gas is reformed together, in order to generate the third gas for including hydrogen.Particularly, third gas contains an a certain proportion of oxidation Carbon, carbon dioxide, water and nitrogen.Reformer carries out heat exchange with afterburner, therefore afterburner may be used as reformer Heater.
Another fuel processor element is so-called water-gas shift reactor.The first gas of third gas and addition The 4th gas for including low ratio carbon monoxide is converted into water-gas shift reactor.4th gas and further addition First gas be introduced in together in so-called PrOx reactors (another fuel processor element), be converted into there 5th gas.In PrOx reactors, the content of carbon monoxide is further decreased, especially by preferred oxidizing carbon monoxide To further decrease the content of carbon monoxide.Then the 5th gas generated in PrOx reactors can be introduced into fuel electricity Chi Zhong.5th gas contains hydrogen, and electric energy and water are obtained from the 5th gas using the oxidant in fuel cell.
In addition, fuel processor includes at least first heat exchanger, which is arranged with it can be right Evaporator is heated.In addition, fuel processor includes the startup burner that can utilize fuel handling.In step a) and b) In, first heat exchanger, then is heated by the first gas that makes to be heated cycle, by the first gas flowed into evaporator Make the first gas cycle through the reformer in fuel processor element, water-gas shift reactor and PrOx reactors by Fuel processor element heats.The first gas heated for flowing through afterburner heats reformer.This method is only Utilize the element that can be also used in the maintenance operation of fuel cell system.This method does not generate the behaviour of fuel cell equipment Any foreign matter made, especially any soot particle.
Preferably, this method further includes being introduced into fuel in the downstream for starting burner and being introduced into afterburner The step of hydrogen and fuel afterburning.Fuel is further supplied to afterburner and increases gas of the guiding by first heat exchanger The temperature of body and the heat for increasing reformer.
In another configuration, this method further includes, in step c)：Use the first heat exchanger with catalyst coatings And it is introduced into fuel in the downstream of afterburner and is catalyzed burning fuel in the first heat exchanger with catalyst coatings.First Catalysis burning in heat exchanger produces the further heat that can directly use and (in this case, be used for heating evaporation device) Amount.This makes the first gas for flowing through evaporator reach raised temperature.
Suitably, used fuel is the mixture of propylene glycol/water.Used first gas is preferably air.
Suitably, fuel processor includes second heat exchanger, and the second heat exchanger is to starting the of burner upstream One gas heat and cooled down to the gas in reformer downstream and water-gas shift reactor upstream.Therefore, first gas It can be preheated starting burner upstream, especially since step d)；Meanwhile it can be in each fuel processor The temperature curve of restriction is established between element.
In a kind of especially preferred configuration, in starting burner, optionally, heating equipment is electrically heated or fuel It is burnt by catalysis.Heating equipment is set in starting burner and again increases fuel cell for be catalyzed the unit to burn and sets Standby degree of integration, because in this way can be to avoid other individually unit.
In a kind of suitable configuration, it can also be connected during the operation of fuel cell and start burner.If first Gas continues to flow through startup burner, then undesirable reflux can be avoided it is not necessary that other element is arranged, especially It is the reflux of hydrogen.
The present invention additionally relates to a kind of fuel cell system with fuel processor and fuel cell, including：
Evaporator,
It is arranged in the reformer in evaporator downstream,
Water-gas shift reactor,
PrOx reactors, and
First heat exchanger,
Wherein, fuel processor includes starting burner and being arranged in PrOx reactor downstreams and first heat exchanger The downstream afterburner of trip, wherein there is first heat exchanger the heat with evaporator to transmit connection.Therefore, it is possible to use The heat of generation is used for the evaporation of fuel.More particularly, the heat generated is used in the place needed.This improves combustions Expect the efficiency of battery apparatus.
" heat transmits connection " in the context of the present invention is construed as meaning the member transmitting connection with heat Heat exchange occurs between part.Suitably, there are two elements that heat transmits connection to be arranged in shared shell or heap each other Folded or one of element is integrated into another element.
Preferably, it includes heating equipment for being heated to first gas and for being carried out to fuel to start burner It is catalyzed the unit of burning.Heating equipment may include heat storage facility and/or electric heating unit.Therefore, burner had been started both It is suitable for generating the low temperature for the first startup stage, is also suitable for generating the higher temperature for the second startup stage.It is this During the startup burner of design can also be otherwise used in the operation of fuel cell, temperature for adjusting fuel cell system or For adjusting the discharge gas for coming from fuel cell.
Fuel cell system according to the present invention realizes highly integrated.Waste heat can be utilized in optimal manner.Fuel Battery apparatus can be operated in a manner of ashless.This significantly reduces the intensity of the maintenance work for fuel cell system.
In a kind of advantageous configuration, start burner at least have there are one first chamber and a second chamber, first There are chamber the catalyst coatings for being catalyzed burning, second chamber to be designed for the preheating of gas.First chamber can be with cloth It sets in second chamber.Catalyst coatings are suitable for burning atomization or evaporation propylene glycol/water mixture.Preferably, it is also suitable for In the burning of hydrogen.If there is insufficient negative pressure, This feature ensures that can be burnt by starting without unburned hydrogen Device is escaped from fuel cell system.
Preferably, the unit for fuel atomizing or evaporation is connected to the upstream for the first chamber for starting burner.With In atomization or evaporation the unit can be start burner a part.
Suitably, first heat exchanger includes the unit of the catalysis burning for fuel.The unit especially may include interior The catalyst coatings of the catalyst coatings on surface and/or the plate being arranged in first heat exchanger, the fuel catalytic on the catalyst coatings Burning.
In another suitable configuration, there is afterburner hot transmit with reformer to connect.Therefore, reformer can be with It is heated by afterburner.
" heat transmits connection " in the context of the present invention should be understood to mean the member transmitting connection with heat Heat exchange occurs between part.Suitably, there are two elements that heat transmits connection to be arranged in shared shell or heap each other It is folded, or wherein element is integrated into another element.
In another arrangement, there is the heat with the second evaporator to transmit and connect for PrOx reactors, the design of the second evaporator At the evaporation for fuel, wherein the fuel being evaporated can be introduced in the upstream of reformer.In PrOx reactors, by PrOx reactions generate heat, preferably generate heat by oxidation reaction.Therefore the heat generated can be used for the further of fuel Evaporation.Which further enhances the efficiency of fuel cell system.
Suitably, second heat exchanger is arranged in startup burner upstream, and second heat exchanger is designed to for cooling down The contraflow heat exchanger of the gas in reformer downstream and water-gas shift reactor upstream.Second heat exchanger can be right simultaneously The gas (i.e. third gas) for leaving reformer is cooled down before it enters in water-gas shift reactor, and simultaneously to wanting It is introduced in the first gas started in burner, especially air is preheated.
In another configuration, water-gas shift reactor is connected to third heat exchanger, third heat exchanger designs at It is preheated in first gas, wherein starting first be provided between burner and afterburner for being heated The supply line of gas.Therefore, the third heat exchanger is for cooling down water-gas shift reactor, while to will be by The first gas being introduced into afterburner is heated.
Suitably, the downstream of PrOx reactors is provided with triple valve, coming from the discharge gas of PrOx reactors can lead to Cross the triple valve be introduced to start burner upstream, by the bypass of fuel cell be introduced to startup burner downstream, Or the downstream for starting burner is introduced to by fuel cell.
This triple valve can back and forth switch between the different operating states of fuel cell system.The valve increases fuel The degree of integration of battery apparatus.When the discharge gas for coming from PrOx reactors is guided to startup burner upstream, fuel treatment Device element can be initially heated to the first operation temperature so that can be with the reaction in starting fluid processor elements.By means of It is guided by bypassing, the reaction in fuel processor element can be adjusted so that the discharge gas for coming from PrOx reactors has The necessary ingredient for being introduced into fuel cell.Fuel cell is connected, the operation of fuel cell is started.
In another configuration, starts burner and be arranged between second heat exchanger and afterburner inline.Start Therefore burner is fully integrated in in the configuration of fuel cell system.
Description of the drawings
Below with reference to attached drawing, the present invention is described in detail.These attached drawings are schematic diagrames.The figures illustrate：
Fig. 1 is the structure of the fuel cell system according to the present invention with fuel processor,
Fig. 2 is the schematic diagram of fuel processor,
Fig. 3 is the flow diagram of the fuel cell system with fuel processor,
Fig. 4 is the flow diagram of the fuel processor during the first stage for starting method,
Fig. 5 is the flow diagram in the catalysis combustion conditions started in burner,
Fig. 6 is the flow diagram in sub-load reformation situation, and
Fig. 7 is the flow diagram in fuel battery operation situation.
Specific implementation mode
Fig. 1 shows the main element of the fuel cell system 1 including fuel processor 2 and fuel cell 70.At fuel It includes following fuel processor element to manage device 2：First evaporator 10, reformer 20, water-gas shift reactor 30 and PrOx are anti- Answer device 40.Fuel B is evaporated by the first evaporator 10.The second gas come out from the first evaporator 10 is indicated by reference numeral G2. It is introduced in reformer 20 together with second gas G2 and first gas G1, it is converted to third gas in reformer 20 G3.Third gas G3 can be introduced in together with the first gas G1 of addition in water-gas shift reactor 30, be turned in water-gas It changes its in reactor 30 and is converted to the 4th gas G4.4th gas G4 can be introduced in together with the first gas G1 of addition In PrOx reactors 40.Discharge gas from PrOx reactors 40 forms the 5th gas that be directed into fuel cell 70 G5.The discharge gas formed in fuel cell 70 is the 6th gas G6, the first gas G1 and/or of the 6th gas G6 and addition Two gas G2 burn in afterburner 21 together.In order to start the fuel cell system 1 shown, need to start burner 50.
Fig. 2 shows fuel processors 2 comprising the first evaporator 10, reformer 20, water-gas shift reactor 30, PrOx reactors 40 start burner 50, afterburner 21 and first heat exchanger 11.These fuel processor elements are with front The sequence mentioned is fluidly coupled to each other.Each in these fuel processor elements all has shell, entrance and exit.It is more special Not, in addition each element also has second entrance.First evaporator 10 and first heat exchanger 11 are arranged so that the first steaming Hair device 10 can be heated by first heat exchanger 11.Reformer 20 and afterburner 21 are connected to each other so that reformer 20 can be with It is heated by afterburner 21.The discharge gas for coming from first heat exchanger 11 is exported from fuel cell system 1.PrOx reactors 40 Include second outlet for releasing the gas into fuel cell 70 or connects between burner 50 in PrOx reactors and starting The pipeline connect, the pipeline have pipeline branch, particularly, have valve.It is arranged between burner 50 and afterburner 21 starting There is another entrance, PrOx reactors 40 can be connected via another entrance or hydrogen can be introduced.
Fig. 3 shows the Working Examples of fuel cell system 1 in schematic form.First evaporator 10 has and first The heat of heat exchanger 11 transmits connection.Optionally, in addition, the 4th heat exchanger 12 can have the heat with the first evaporator 10 to pass Pass connection.Fuel B is introduced in the first evaporator 10.The outlet for coming from the first evaporator 10 has via first pipe L1 It is connected to fluidly connecting for reformer 20.First gas G1 is introduced by leading to the second pipe L2 in first pipe L1 In one pipeline L1.Second pipe L2 is connected to the 4th heat exchanger 12.The third gas G3 generated in reformer 20 is guided Second heat exchanger 60 is reached by third pipeline L3, and then reaches the downstream of second heat exchanger 60, passes through the 4th pipeline L4 enters in water-gas shift reactor 30.Pipeline for supplying first gas G1 can be led in the 4th pipeline L4.In water- The 4th gas G4 generated in gas shift reactor 30 is conducted through the 5th pipeline L5 and enters in PrOx reactors 40.For The supply department of first gas G1 can lead in the 5th pipeline L5.Water-gas shift reactor 30 has and third heat exchanger 31 Heat transmit connection.
PrOx reactors 40 have another entrance for introducing first gas G1.In the configuration shown, PrOx reactions There is device 40 heat with the second evaporator 41 to transmit connection.In this way, the heat that generated in PrOx reactors 40 can be removed.The Two evaporators 41 include supply department for being introduced into fuel B and lead to the outlet in first pipe L1 via the 6th pipeline L6.The One evaporator 10 and the second evaporator 41 can alternatively or additionally take the form of superheater.
The discharge gas (i.e. the 5th gas G5) generated in PrOx reactors 40 is directed to triple valve 80 via the 7th pipeline L7. Three pipelines are branched out from triple valve 80：The 8th pipeline L8 for leading to the supply department for starting burner 50 is guided to from triple valve 80, The supply department is expressed as the 12nd pipeline with reference numeral L12；The 9th pipeline L9 of the supply department for leading to afterburner 21 is led to, The supply department is the 13rd pipeline L1；And the tenth pipeline L10 of fuel cell 70 is guided to from triple valve 80.Come from fuel electricity The discharge gas in pond 70 guides to the 13rd pipeline L13 via the 11st pipeline L11.9th pipeline L9 and the 11st pipeline L11 can be with It combines with each other so that the only one in the two pipelines L9, L11 is passed through in the 13rd pipeline L13.
5th gas G5 or first gas G1 are introduced by the 12nd pipeline L12 to be started in burner 50, the 5th gas G5 Or first gas G1 burns or is heated in starting burner 50.Come from the discharge gas for starting burner 50 and/or is opening The air heated in dynamic burner 50 is supplied to afterburner 21 via the 13rd pipeline L13.Come from afterburner 21 Gas is discharged optionally to be directed in first heat exchanger 11 together with the other fuel B with addition via the 14th pipeline L14, and Heat exchanger 11 is left as the 7th gas G7.
First heat exchanger 11 has the unit of the catalysis burning for fuel B.For being urged in first heat exchanger 11 The unit for changing burning uses the form for the catalyst coatings for being arranged in the plate in first heat exchanger 11.
It includes the heating equipment that can be electrically heated and the unit of the catalysis burning for fuel B to start burner 50. Start burner 50 and preferably include nozzle (being not shown in figure 3), is used for the atomization or evaporation of fuel B so that can be with more High efficiency realizes burning.Alternatively, it may include another evaporator for fuel vaporization to start burner 50.The tenth The upstream of two pipeline L12, can be countercurrently to guide first gas G1 to pass through second heat exchanger 60 so that can will be heated First gas G1 guiding enter and start in burner 50.
Fig. 4 shows the fuel processor element of the fuel cell system 1 of the first startup stage needs with flow diagram, with And corresponding gas conduction.In the first startup stage for heating fuel processor element, only first gas G1 is drawn Fuel processor element was connected.First gas G1 is conducted through the first evaporator 10 or is evaporated suitably by with first Device 10 has hot linked 4th heat exchanger 12.The second heat that first gas G1 continues through reformer 20, there can optionally be Exchanger 60, water-gas shift reactor 30 and PrOx reactors 40, and guide to and start in burner 50 from PrOx reactors 40. Starting burner 50 has heating equipment and using heating equipment heating first gas G1.It is heated in starting burner 50 First gas G1 flow through afterburner 21 and first heat exchanger 11.First heat exchanger 11 transfers heat to the first evaporation Device 10 and existing any 4th heat exchanger 12.Afterburner 21 heats reformer 20.
When there are when second heat exchanger 60, can other first gas G1 being introduced into 12 upstream of the 12nd pipeline In second heat exchanger 60.The element of fuel processor 2 is set to reach the first temperature T1 by the processing step.
The second startup stage was shown with flow diagram in Figure 5.It will start burner 50 by the catalysis burning of fuel B It is heated to second temperature T2.First gas G1 passes through the first evaporator 10 or the 4th heat exchanger 12.The sky heated wherein Gas continues to flow through reformer 20, optional second heat exchanger 60, water-gas shift reactor 30 and PrOx reactors 40, and by It is introduced into the 12nd pipeline L12 for starting 50 upstream of burner.Then, the fuel B for being atomized or evaporating is in starting burner 50 Catalysis burning.It is alternatively possible to carry out other electrical heating to heating equipment.Come from start burner 50 discharge gas via 13rd pipeline L13 guides to afterburner 21.It is alternatively possible to which other fuel B is introduced into the 13rd pipeline L13.It comes from It burns in afterburner 21 in any fuel B for starting the discharge gas of burner 50 and being introduced into.As shown in Figure 5, if after There is burner 21 heat with reformer 20 to transmit connection, then the waste heat for coming from afterburner 21 can be utilized further to heat Reformer 20.The discharge gas for coming from afterburner 21 guides to first heat exchanger 11 via the 14th pipeline L14.With use In the first heat exchanger 11 of the unit of catalysis burning, additionally fuel B can be introduced into the 14th pipeline L14, made Obtain the further catalysis burning that fuel B is carried out in first heat exchanger 11.The gas for having been moved off first heat exchanger is Seven gas G7.The waste heat of generation is additionally operable to the first evaporator 10 of heating and optional 4th heat exchanger 12.
Fig. 6 shows the flow diagram that the so-called sub-load after the second startup stage is reformed, and fires during this period Expect that battery is connected not yet.In the processing step, fuel B is additionally introduced into the first evaporator 10.Further, it is also possible to Fuel B is introduced into the second evaporator 41.In the processing step, each element of the reaction of conception in fuel processor 2 Middle progress, i.e. reformer 20, water-gas shift reactor 30 and PrOx reactors 40.Come from the discharge gas of PrOx reactors 40 (i.e. the 5th gas G5) is introduced in the processing stage starts the 13rd of 50 downstream of burner and 21 upstream of afterburner In pipeline L13.In the processing step, starts burner 50 and any upstream second heat exchanger 60 and be used to supply the heated One gas G1.First gas G1 can further be heated alternately through the electrical heating of heating equipment by starting burner 50.
It is by the way that first gas G1 to be supplied in the 5th pipeline L5 or by the to implement reaction in PrOx reactors 40 One gas G1 is supplied to by other entrance to be completed in PrOx reactors 40.
In order to terminate the startup method or for the complete operation of fuel cell system 1, fuel cell 70 is connected to Fuel processor 2.This means that the discharge gas for coming from PrOx reactors 40 is introduced into fuel cell 70.This is in the figure 7 It shows.The discharge gas for coming from fuel cell 70 is recycled to and opens especially from the anode discharge gas in fuel cell 70 In the fuel processor 2 of dynamic 21 upstream of 50 downstream of burner and afterburner.Further reaction in fuel processor 2 continues It is carried out in reformer 20, water-gas shift reactor 30 and PrOx reactors 40.Fuel cell be discharged gas optionally with addition Fuel B is subjected to afterburning or together with the further fuel B of addition in first heat exchanger 11 in afterburner 21 together Middle catalysis burning.7th gas G7 is removed from heat exchanger 11.Also in the processing step, optionally pre-warmed first gas Body G1, which is still flowed through, starts burner 50.
Reference numerals list
1 fuel cell system
2 fuel processors
10 first evaporators
11 first heat exchangers
12 the 4th heat exchangers
20 reformers
21 afterburners
30 water-gas shift reactors
31 third heat exchangers
40 PrOx reactors
41 second evaporators
50 start burner
60 second heat exchangers
70 fuel cells
80 triple valves
B fuel
G1 first gas
G2 second gas
G3 third gas
The 4th gases of G4
The 5th gases of G5
The 6th gases of G6
The 7th gases of G7
L1 first pipes
L2 second pipes
L3 third pipelines
The 4th pipelines of L4
The 5th pipelines of L5
The 6th pipelines of L6
The 7th pipelines of L7
The 8th pipelines of L8
The 9th pipelines of L9
The tenth pipelines of L10
The 11st pipelines of L11
The 12nd pipelines of L12
The 13rd pipelines of L13
The 14th pipelines of L14
The first temperature of T1
T2 second temperatures

Claims (17)

1. the method for starting fluid battery apparatus (1), the fuel cell system includes fuel processor (2) and fuel cell (70),
Wherein, fuel processor (2) includes following element：First evaporator (10) is arranged in the first evaporator (10) downstream Reformer (20), water-gas shift reactor (30), PrOx reactors (40), first heat exchanger (11), afterburner (21) and Start burner (50),
Wherein, described method includes following steps：
A) heating equipment in fuel processor (2) is electrically heated, first gas (G1) is heated,
B) by the first gas (G1) for making to be heated cycle through at least first heat exchanger (11) and afterburner (21) come The element of fuel processor (2) is heated to fixed operation temperature,
C) it is catalyzed burning atomization or evaporation fuel (B) in starting burner (50), is then mended in afterburner (21) Hydrogen is fired, for further being heated to first gas (G1) via at least one heat exchanger,
D) fuel (B) is introduced into the element of fuel processor (2) being preheated and stops starting urging in burner (50) Change burning,
E) start at least one reaction in the element of fuel processor (2), until the gas come out from PrOx reactors (40) With given CO contents, and
F) fuel cell (70) is connected.
2. according to the method described in claim 1, wherein, step c) includes：
It is introduced into fuel (B) in the downstream for starting burner (50) and afterburning is introduced into hydrogen and fuel in afterburner (21) (B)。
3. method according to claim 1 or 2, wherein step c) includes：
Using the first heat exchanger (11) with catalyst coatings, and
It is introduced into fuel (B) and the catalysis combustion in the first heat exchanger (11) with catalyst coatings in the downstream of afterburner (21) Burn the fuel (B).
4. according to any method of the preceding claims, wherein used fuel (B) is the mixed of propylene glycol/water Close object.
5. according to any method of the preceding claims, wherein used first gas (G1) is air.
6. according to any method of the preceding claims, wherein fuel processor (2) includes second heat exchanger (60), the second heat exchanger will start first gas (G1) heating of burner (50) upstream, and will be under reformer (20) The first gas (G1) or third gas (G3) of trip and water-gas shift reactor (30) upstream are cooling.
7. according to any method of the preceding claims, wherein in starting burner (50), optionally, will add Hot equipment electrical heating and/or by fuel (B) be catalyzed burn.
8. according to any method of the preceding claims, wherein connect and open during the operation of fuel cell (70) Dynamic burner (50).
9. the fuel cell system (1) with fuel processor (2) and fuel cell (70), including：
First evaporator (10),
It is arranged in the reformer (20) in the first evaporator (10) downstream,
Water-gas shift reactor (30),
PrOx reactors (40), and
First heat exchanger (11),
It is characterized in that, fuel processor (2) includes starting burner (50) and being arranged in PrOx reactors (40) downstream and the The downstream afterburner (21) of one heat exchanger (11) upstream.
10. fuel cell system (1) according to claim 9, wherein it includes being used for first gas to start burner (50) (G1) unit of electrically heated unit and the catalysis burning for fuel (B).
11. fuel cell system (1) according to claim 9 or 10, wherein first heat exchanger (11) includes for firing Expect the unit of the catalysis burning of (B).
12. the fuel cell system (1) according to any one of claim 9 to 11, wherein afterburner (21) have with The heat of reformer (20) transmits connection.
13. the fuel cell system (1) according to any one of claim 9 to 12, wherein PrOx reactors (40) have It transmits and connects with the heat of the second evaporator (41), the second evaporator (41) is designed for the evaporation of fuel (B), wherein is steamed The fuel (B) of hair can be introduced in the upstream of reformer (20).
14. the fuel cell system (1) according to any one of claim 9 to 13, wherein second heat exchanger (60) cloth It sets in the upstream for starting burner (50), second heat exchanger (60) is contraflow heat exchanger, is designed to cooled reformer (20) gas in downstream and water-gas shift reactor (30) upstream.
15. the fuel cell system (1) according to any one of claim 9 to 14, wherein water-gas shift reactor (30) it is connected to third heat exchanger, the pairs of first gas of third heat exchanger designs (G1) is preheated, wherein be used for quilt The supply line of the first gas (G1) of heating, which is arranged in, to be started between burner (50) and afterburner (21).
16. the fuel cell system (1) according to any one of claim 9 to 15, wherein in PrOx reactors (40) Downstream is provided with triple valve (80), comes from the discharge gas of PrOx reactors (40) and can be introduced to startup by the triple valve The upstream of burner (50) is introduced to the downstream of startup burner (50) by the bypass of fuel cell (70) or passes through combustion Material battery (70) is introduced to the downstream for starting burner (50).
17. the fuel cell system (1) according to any one of claim 9 to 16, wherein it is inline to start burner (50) Ground is arranged between second heat exchanger (60) and afterburner (21).
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113301988A (en) * 2019-03-15 2021-08-24 三菱动力株式会社 Apparatus and method for processing raw material fluid

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102019110343A1 (en) * 2019-04-18 2020-10-22 e.Go REX GmbH CIRCUIT ARRANGEMENT FOR AN ON-BOARD NETWORK OF AN ELECTRICALLY DRIVEN MOTOR VEHICLE AND A METHOD FOR OPERATING SUCH A CIRCUIT ARRANGEMENT
CN111403772B (en) * 2020-03-06 2020-11-17 电子科技大学 Cold starting device of fuel cell and control method thereof
DE102021100954A1 (en) 2021-01-19 2022-07-21 Schaeffler Technologies AG & Co. KG Test system and method for running in and testing fuel cells

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2448662A1 (en) * 2000-05-31 2001-12-13 Nuvera Fuel Cells, Inc. Joint-cycle high-efficiency fuel cell system with power generating turbine
US20030170510A1 (en) * 2002-03-08 2003-09-11 Robb Gary M. Method for quick start-up of a fuel processing system using controlled staged oxidation
CN1748334A (en) * 2003-01-21 2006-03-15 通用汽车公司 Fuel processing system having a membrane separator
CN1989068A (en) * 2004-07-19 2007-06-27 沃尔沃公司 Method and equipment of fuel reforming
CN101238608A (en) * 2005-05-09 2008-08-06 布卢姆能源公司 High temperature fuel cell system with integrated heat exchanger network
CN101341617A (en) * 2005-12-19 2009-01-07 卡西欧计算机株式会社 Power supply system and control method thereof
CN103236555A (en) * 2012-11-05 2013-08-07 华中科技大学 Solid oxide fuel cell system and thermoelectricity synergic control method
CN107112560A (en) * 2014-12-01 2017-08-29 Ht切拉米克斯有限公司 The method of SOFC systems and operation SOFC systems
CN206907859U (en) * 2017-05-27 2018-01-19 晋城市阿邦迪能源有限公司 Ethanol reformation fuel cell generation

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19754013C2 (en) 1997-12-05 2000-10-26 Dbb Fuel Cell Engines Gmbh Device and method for steam reforming a hydrocarbon
DE19755813C2 (en) * 1997-12-16 2000-09-14 Dbb Fuel Cell Engines Gmbh Process for operating a steam reforming plant, thus operable reforming plant and fuel cell system operating method
EP0924162A3 (en) 1997-12-16 1999-10-20 dbb fuel cell engines GmbH Membrane for the separation of hydrogen, methanol reformer using this membrane and process for its operation
EP1181241B1 (en) * 1999-05-03 2005-08-24 Nuvera Fuel Cells Autothermal reforming system with integrated shift beds, preferential oxidationreactor, auxiliary reactor, and system controls
US6838062B2 (en) * 2001-11-19 2005-01-04 General Motors Corporation Integrated fuel processor for rapid start and operational control
DE10315255A1 (en) * 2003-04-03 2004-10-21 J. Eberspächer GmbH & Co. KG Fuel cell system and burner arrangement for a fuel cell system
DE20320913U1 (en) 2003-12-22 2005-05-19 Truma Gerätetechnik GmbH & Co. KG Reformer fuel cell system for a mobile device/space with a useful storage capacity has a fuel cell to generate electric current via a hydrogen-rich gas and a heating device
ATE443353T1 (en) 2005-03-16 2009-10-15 Truma Geraetetechnik Gmbh & Co REFORMER FUEL CELL SYSTEM WITH EXTERNAL BURNER

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2448662A1 (en) * 2000-05-31 2001-12-13 Nuvera Fuel Cells, Inc. Joint-cycle high-efficiency fuel cell system with power generating turbine
US20030170510A1 (en) * 2002-03-08 2003-09-11 Robb Gary M. Method for quick start-up of a fuel processing system using controlled staged oxidation
CN1748334A (en) * 2003-01-21 2006-03-15 通用汽车公司 Fuel processing system having a membrane separator
CN1989068A (en) * 2004-07-19 2007-06-27 沃尔沃公司 Method and equipment of fuel reforming
CN101238608A (en) * 2005-05-09 2008-08-06 布卢姆能源公司 High temperature fuel cell system with integrated heat exchanger network
CN101341617A (en) * 2005-12-19 2009-01-07 卡西欧计算机株式会社 Power supply system and control method thereof
CN103236555A (en) * 2012-11-05 2013-08-07 华中科技大学 Solid oxide fuel cell system and thermoelectricity synergic control method
CN107112560A (en) * 2014-12-01 2017-08-29 Ht切拉米克斯有限公司 The method of SOFC systems and operation SOFC systems
CN206907859U (en) * 2017-05-27 2018-01-19 晋城市阿邦迪能源有限公司 Ethanol reformation fuel cell generation

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113301988A (en) * 2019-03-15 2021-08-24 三菱动力株式会社 Apparatus and method for processing raw material fluid
CN113301988B (en) * 2019-03-15 2023-10-20 三菱重工业株式会社 Raw material fluid treatment apparatus and raw material fluid treatment method
US11939915B2 (en) 2019-03-15 2024-03-26 Mitsubishi Heavy Industries, Ltd. Raw material fluid treatment plant and raw material fluid treatment method

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US20180241057A1 (en) 2018-08-23
DE102017001564A1 (en) 2018-08-23
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